WO2010006465A1 - 一种循环流化床制备二硫化碳的设备 - Google Patents

一种循环流化床制备二硫化碳的设备 Download PDF

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Publication number
WO2010006465A1
WO2010006465A1 PCT/CN2008/001321 CN2008001321W WO2010006465A1 WO 2010006465 A1 WO2010006465 A1 WO 2010006465A1 CN 2008001321 W CN2008001321 W CN 2008001321W WO 2010006465 A1 WO2010006465 A1 WO 2010006465A1
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Prior art keywords
fluidized bed
heating furnace
riser
settler
carbon
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PCT/CN2008/001321
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English (en)
French (fr)
Inventor
孔庆然
卢春喜
王祝安
王捷
刘梦溪
康和平
Original Assignee
上海百金化工集团有限公司
中国石油大学(北京)
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Application filed by 上海百金化工集团有限公司, 中国石油大学(北京) filed Critical 上海百金化工集团有限公司
Priority to PCT/CN2008/001321 priority Critical patent/WO2010006465A1/zh
Publication of WO2010006465A1 publication Critical patent/WO2010006465A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/70—Compounds containing carbon and sulfur, e.g. thiophosgene
    • C01B32/72—Carbon disulfide

Definitions

  • the present invention relates to a production apparatus for a compound containing carbon and sulfur, and more particularly to an apparatus for preparing carbon disulfide in a circulating fluidized bed.
  • Carbon disulfide is an important chemical raw material and has a wide range of applications in the industry. It is widely used in the production sectors of man-made fibers, cellophane, pesticides, carbon tetrachloride, rubber, and petroleum refining.
  • the methods for producing carbon disulfide mainly include charcoal sulfur method, coke sulfur method and methane sulfur method, and the processes used are classified into a fixed bed process and a fluidized bed process.
  • a single fixed bed reactor with indirect heating is widely used in China.
  • the method has the problems of high energy consumption, low equipment production capacity, large floor space, serious pollution environment, high labor intensity, etc., and semi-coke or coke and Sulfur mass transfer, poor heat transfer efficiency, high energy consumption, more importantly, semi-coke or coke and sulfur have a small contact area, insufficient contact, incomplete reaction, and need to intermittently add coke according to the degree of reaction, unable to achieve continuous production Chemical.
  • the patent documents of Chinese Patent Nos. 200610102044.0 and 200510129940.1 propose a fluidized bed production process of carbon disulfide, which uses two fluidized beds, one as a reactor and the other as a burner, semi-coke or lignite burning. Burning in the device, releasing a large amount of heat, the unburned semi-coke or lignite entrained part of the heat is transferred from the transfer line into the fluidized bed reactor, and the gaseous sulfur is transported into the fluidized bed reactor to react with the high temperature semi-coke or lignite.
  • the generated carbon disulfide gas enters the two-stage cyclone separator to separate the entrained semi-coke or lignite powder, and then enters the subsequent separation equipment; the unreacted semi-coke or lignite is circulated into the fluidized bed burner for further combustion.
  • the above fluidized bed process and equipment greatly improve the production efficiency of carbon disulfide, there are still some shortcomings: (1) In the fluidized bed process, the particle conveying pipe is two U-shaped pipes, and the transportation of the particles is extremely difficult; In the chemical bed process, the carbon-containing solid particles stay in the reactor for a long time, and the heat balance is difficult to maintain; (3) the sulfur must be gasified, so a set of sulfur needs to be set.
  • the gasification device makes the whole process more complicated and the equipment investment increases. (4) The unreacted semi-coke or lignite directly enters the fluidized bed burner, and the entrained large amount of carbon disulfide gas is not removed, which reduces the product. yield, and carbon disulfide in a fluidized bed combustor burning after releasing large amounts of SO x, pollution of the environment.
  • the present invention provides an apparatus for preparing carbon disulfide in a circulating fluidized bed.
  • the invention is realized by the following technical scheme: a device for preparing carbon disulfide in a circulating fluidized bed, comprising a silo, a feeder and a fluidized bed heating furnace connected by a pipeline and a feeder, wherein the fluidized bed heating furnace is provided with heat.
  • Charcoal pipeline the other end of the hot carbon pipeline is connected with the pre-lifter, a riser is connected above the pre-lifter, a nozzle is arranged on the riser, the upper end of the riser extends into the settler, and a quick-distribution device is arranged at the end, and the top of the settler is provided
  • the cyclone separator has a stripping section inside and below, and a cold carbon line connected to the fluidized bed heating furnace is arranged below the stripping section.
  • the stripping process of the stripping section is to replace the carbon disulfide gas entrained between the semi-coke particles and the carbon disulfide gas adsorbed in the micropores of the semi-coke particles with an inert gas, so as to prevent the carbonaceous solid matter entraining a large amount of carbon disulfide gas and burning into the heating furnace. , 'generate a large amount of so x while reducing product yield.
  • the function of the pre-lifter is to raise the carbonaceous solid matter from the hot carbon pipeline to move upwards and form an ideal plug flow to improve the contact efficiency of the atomized liquid sulfur and the carbonaceous solid matter from the nozzle. .
  • the carbon-containing solid matter in the silo is sent to the fluidized bed heating furnace through the feeder, and after burning and aerating by air, a part of the carbon-containing solid matter is burned off, and the heat is released to heat the remaining carbon-containing solid matter; the heated carbon-containing solid matter Passing through the hot carbon line into the pre-lifter, then entering the riser and flowing upwards; gaseous or liquid sulfur is sprayed into the riser from the nozzle, in contact with high temperature carbonaceous solid matter and reacting to form gaseous carbon disulfide; fast splitting at the end of the riser
  • the device separates the generated gaseous carbon disulfide from the unreacted carbonaceous solid matter, and the separated gaseous carbon disulfide entrained part contains carbon solid matter into the settler, and then enters the cyclone separator to separate the entrained carbonaceous solid matter, and the settler Top discharge, after entering a continuous separation system; the unreacted carbonaceous solid material separated by the fast separation device falls into the strip
  • Burning in the furnace In order to avoid the problem of environmental pollution caused by insufficient combustion of carbon-containing solid matter in the fluidized bed heating furnace, and then directly discharging air into the air, people can use various methods to treat the generated high-temperature flue gas. It is well known to those of ordinary skill in the art.
  • the device of the present invention comprises two forms, a side-by-side and a coaxial type, wherein the side-by-side structure is as follows:
  • the fluidized bed heating furnace and the settler are arranged side by side, wherein the pre-lifter, the riser and the settler are coaxially arranged
  • the order from bottom to top is: pre-lifter, riser and settler; the upper end of the riser is directly inserted into the lower part of the settler, and the hot carbon line and the cold carbon line are inclined pipes respectively. If the space is not enough, the cold carbon line and The inlet and outlet of the hot 'carbon line are set as inclined pipes and the middle is straight pipes.
  • the specific structure of the coaxial type is as follows:
  • the fluidized bed heating furnace is arranged coaxially with the settler, wherein the pre-lifter is arranged coaxially with the riser, the settler is located above the fluidized bed heating furnace, and the riser is composed of a vertical pipe and a horizontal pipe
  • the front end of the horizontal pipe extends into the settler, and the cold carbon line is disposed in the fluidized bed heating furnace, and an anti-back cone is arranged at the outlet to prevent the gas in the fluidized bed heating furnace from entering the cold carbon line.
  • the hot carbon line is composed of a vertical tube and a inclined tube.
  • the angle between the cold charcoal line and the stripping section axis at the junction with the stripping section is controlled at
  • the structure of the fluidized bed heating furnace of the present invention has three structural forms, one is that the upper part of the fluidized bed heating furnace has the same diameter as the lower part; the other is that the upper diameter is smaller than the lower diameter to increase the dilute phase velocity, artificially reducing the cyclone
  • the separator efficiency is to discharge the fly ash after combustion; the third is that the lower diameter is smaller than the upper diameter, mainly to reduce the velocity of the dilute phase gas, reduce the entrained particle concentration, and improve the efficiency of the cyclone separator.
  • a fluidized bed is added in the middle of the riser for the purpose of prolonging the reaction time.
  • the diameter of the fluidized bed is larger than the diameter of the riser, and the diameter and size of the fluidized bed are The required reaction time is determined; to maintain the fluidized bed level, below the fluidized bed and settler
  • the stripping sections are connected by a circular tube, and the round tube is provided with a valve.
  • the cold carbon line and/or the hot carbon line are respectively equipped with a control valve, which may be a spool valve or a plug valve or other valve for controlling the flow rate of high-temperature particles; when the equipment is arranged side by side
  • a control valve which may be a spool valve or a plug valve or other valve for controlling the flow rate of high-temperature particles
  • the cyclone separator is an outer cyclone separator or an inner cyclone separator, the cyclone separator is internally provided with an insulated and wear-resistant lining, the cyclone separator is a first-stage cyclone separator, or a multi-stage cyclone separator is connected in series, wherein each stage
  • the cyclone separator is one or more, and the specific number is determined by the gas flow rate and the size of the settler in the settler;
  • the quick-distribution device is a gas-solid separation device such as a cyclone separator or a trilobal quick-dividing or swirling fast-dividing.
  • the present invention has the following advantages:
  • the pre-lifter and the riser are used to make the carbonaceous solid material fully contact with the liquid or gaseous sulfur in the riser and react, and at the same time, the fluidized bed in the middle of the riser makes the reaction proceed more thoroughly, greatly improving the reactants. Contact efficiency increases the yield of the product;
  • the sulfur of the present invention can be liquid, not only requires lower temperature, low energy consumption, but also requires simple equipment and small footprint. , reduce production costs;
  • the stripping section is set so that the two fluidized carbon gas entrained in the unreacted carbon-containing solid matter is stripped off, effectively avoiding a large amount of carbon disulfide gas entering the heating furnace, generating a large amount of S0 X , thereby reducing pollution and protecting the environment. At the same time, the product yield is improved;
  • the whole device has simple structure, low material cost, low cost and easy production. It is conducive to continuous and automatic production and is beneficial to the environmental protection of the production process.
  • the use of the apparatus of the present invention to produce carbon disulfide is technically and economically the best choice, truly achieving the goals of energy saving, consumption reduction, cleaning, and environmental protection.
  • FIG. 1 is a schematic diagram of the side-by-side structure of the present invention
  • FIG. 3 is a schematic diagram of the side-by-side structure of the present invention
  • Figure 5 is a schematic view of the coaxial structure of the present invention
  • Figure 6 is a schematic view of the coaxial structure of the present invention
  • Embodiment 1 As shown in FIG. 1, the parallel structure according to the present invention
  • the apparatus for preparing carbon disulfide in a circulating fluidized bed comprises a silo 1, a feeder 2, and a fluidized bed heating furnace 3 connected to the feeder 2 through a pipeline.
  • the lower diameter of the fluidized bed heating furnace is smaller than the upper diameter;
  • the fluidized bed heating furnace 3 is provided with a hot carbon line 4 below, and the other end of the hot carbon line 4 is connected with the pre-lifter 5, and a riser 6 is connected above the pre-lifter 5, and a nozzle 7 is arranged on the riser 6, and the upper end of the riser 6 is extended into the settling
  • the quick-distribution device 9 is arranged at the end, the quick-distribution device is a cyclone separator, the cyclone separator 10 is arranged at the top of the settler, the stripping section 11 is disposed at the lower part, and the fluidized bed is arranged below the stripping section 11
  • the side-by-side structure is embodied in a fluidized bed heating furnace 3 and a settler 8 arranged side by side, wherein the pre-lifter 5, the riser 6 and the settler 8 are coaxially arranged, and the upper end of the riser 6 is directly inserted into the settlement.
  • the hot carbon line 4 and the cold carbon line 12 are respectively inclined tubes, and the angle between the cold charcoal line 12 and the stripping section axis is controlled between 20° and 60° with the stripping section 11 and is heated by the fluidized bed.
  • the angle of the hot carbon line 4 at the junction of the furnace 3 and the axis of the fluidized bed heating furnace is controlled between 20° and 60°.
  • the carbon-containing solid matter in the silo is sent to the fluidized bed heating furnace through the feeder, After fluidizing and burning, the air burns off a part of the carbon-containing solid matter, and releases heat to heat the remaining carbon-containing solid matter; the heated carbon-containing solid material enters the pre-lifter through the hot carbon line, then enters the riser and flows upward; gaseous or liquid sulfur Sprayed into the riser by the nozzle, contacted with high temperature carbon-containing solid matter and reacted to form gaseous carbon disulfide; the quick-distribution device disposed at the end of the riser separates the generated gaseous carbon disulfide from the unreacted carbonaceous solid matter and separates it.
  • the gaseous carbon disulfide entrained part of the carbon-containing solid matter enters the settler, and then enters the cyclone separator to separate the entrained carbonaceous solid matter, which is discharged from the top of the settler and enters the subsequent separation system; the unreacted content separated by the quick separation device
  • the carbon solid matter falls into the stripping section below the settler, and the entrained carbon disulfide is stripped by the inert gas and then burned into the fluidized bed heating furnace by the cold charcoal line.
  • Embodiment 2 As shown in FIG. 2, the parallel structure of the present invention
  • the upper diameter of the fluidized bed heating furnace is smaller than the lower diameter.
  • the efficiency of the cyclone separator is artificially reduced to increase the efficiency of the cyclone, and the fly ash after combustion is discharged.
  • Embodiment 3 As shown in FIG. 3, the parallel structure of the present invention
  • Embodiment 1 The difference from Embodiment 1 is that the fluidized bed layer 14 is added in the middle of the riser 6 to prolong the reaction time.
  • the diameter of the fluidized bed is larger than the diameter of the riser.
  • the diameter of the fluidized bed and its size are determined by the required reaction time.
  • the fluidized bed and the stripping section below the settler are connected by a circular tube, and a valve is arranged on the round tube to control the flow rate of the material.
  • Embodiment 4 As shown in FIG. 4, the parallel structure of the present invention
  • Embodiment 3 The only difference from Embodiment 3 is that the upper diameter of the fluidized bed heating furnace is smaller than the lower diameter.
  • Embodiment 5 As shown in FIG. 5, the coaxial structure of the present invention
  • the apparatus for preparing carbon disulfide in a circulating fluidized bed comprises a silo 1, a feeder 2, and a fluidized bed heating furnace 3 connected to the feeder 2 through a pipeline, and a hot carbon pipeline 4 is disposed under the fluidized bed heating furnace 3, and the hot carbon pipeline is provided.
  • the other end is connected with the pre-lifter 5
  • the riser 6 is connected with a riser 6 above
  • the riser 6 is provided with a nozzle 7
  • the upper end of the riser 6 extends into the settler 8
  • the quick branch device 9 is arranged at the end
  • the fast split The device is three
  • the leaf shape is fast divided
  • the top of the settler is provided with a cyclone separator 10
  • the bottom part is provided with a stripping section 11
  • the stripping section 11 is provided with a cold carbon line 12 connected to the fluidized bed heating furnace 3
  • a control valve 16 is mounted on the hot carbon line 4, respectively.
  • the coaxial structure is embodied in a coaxial arrangement between the fluidized bed heating furnace 3 and the settler 8, wherein the pre-lifter 5 is arranged coaxially with the riser 6, and the settler 8 is located in the fluidized bed heating furnace 3.
  • the riser 6 is composed of a vertical pipe and a horizontal pipe, and the front end of the horizontal pipe extends into the settler, and the cold carbon line 12 is disposed in the fluidized bed heating furnace 3, and an anti-back cone 13 is arranged at the outlet thereof, and the hot carbon pipeline 4 is provided. It consists of a standpipe and a tilted pipe.
  • the carbon-containing solid matter flow path, the sulfur feed mode, the reaction, and the combustion mode that is, the entire preparation process are consistent with the side-by-side.
  • Embodiment 6 As shown in FIG. 6, the coaxial structure of the present invention
  • the only difference from the embodiment 5 is that the fluidized bed layer 14 is added in the middle of the riser pipe of the riser 6 to prolong the reaction time.
  • the diameter of the fluidized bed layer is larger than the diameter of the riser pipe, and the diameter of the fluidized bed layer and its size are required.
  • the reaction time is determined; in order to maintain the fluidized bed level, the fluidized bed is connected to the stripping section below the settler through a circular tube 15, which is provided with a valve 17. '

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Description

一种循环流化床制备二硫化碳的设备
技术领域
本发明涉及一种含碳和硫的化合物的生产设备， 具体为一种循环流化床制 备二硫化碳的设备。
背景技术
二硫化碳是一种重要的化工原料，在工业上有着广泛的用途， 在人造纤维、 玻璃纸、 农药、 四氯化碳、 橡胶、 石油炼制等生产部门都有广泛的应用。 目前 生产二硫化碳的方法主要有木炭硫磺法、 焦炭硫磺法和甲烷硫磺法， 所采用的 工艺分为固定床工艺和流化床工艺。 目前国内普遍采用的是间接加热的单台固 定床反应器， 该方法存在着能耗高、 设备生产能力低、 占地面积大、 污染环境 严重、 劳动强度大等问题； 而且半焦或焦炭与硫磺传质、传热效率差， 能耗高， 更重要的是半焦或焦炭与硫磺的接触面积小、 接触不充分、 反应不完全， 而且 需要根据反应程度间歇加焦， 无法实现生产的连续化。
相比于固定床工艺， 流化床工艺使二蔬化碳的生产有了质的提高。 中国专 利号为 200610102044.0和 200510129940.1的专利文献里提出了一种二硫化碳的 流化床生产工艺， 该专利采用了两个流化床， 一个作为反应器， 另一个作为燃 烧器， 半焦或褐煤在燃烧器中燃烧， 放出大量热量， 未烧完的半焦或褐煤夹带 这部分热量由输送管线进入流化床反应器，气态硫磺被输送进入流化床反应器， 与高温半焦或褐煤发生反应， 生成的二硫化碳气体进入两级旋风分离器分离掉 夹带的半焦或褐煤粉末， 然后进入后续分离设备； 未反应完的半焦或褐煤循环 进入流化床燃烧器进一步燃烧。 上述流化床工艺及设备尽管大大提高了二硫化 碳的生产效率， 但依然存在一些缺点： （1)流化床工艺中颗粒输送管是两个 U 形管， 颗粒的输送极为困难； （2)流化床工艺中含碳固体颗粒要在反应器中停留 较长时间，热平衡难以维持； (3)硫磺必须要进行气化， 因而需要设置一套硫磺
确认本 气化装置，使全装置流程更加复杂、设备投资增加；.(4)未反应完的半焦或褐煤 直接进入流化床燃烧器， 其中夹带的大量二硫化碳气体未能得到脱除， 降低了 产品产率，而且二硫化碳在流化床燃烧器内燃烧后释放出大量 SOx，污染环境。
实用新型内容
本发明为了解决现有二硫化碳生产工艺及设备存在上述各种各样的缺点， 提供一种循环流化床制备二硫化碳的设备。
本发明是采用如下技术方案实现的：一种循环流化床制备二硫化碳的设备, 包括料仓、 加料器以及通过管线与加料器连接的流化床加热炉， 流化床加热炉 下方设有热炭管线， 热炭管线另一端与预提升器连通， 预提升器上方连有提升 管， 提升管上设有喷嘴， 提升管上端伸入沉降器， 末端设置快分装置， 沉降器 内顶部设有旋风分离器， 内下方设有汽提段，汽提段下方设有与流化床加热炉 连通的冷炭管线。 所述汽提段的汽提过程是用惰性气体将半焦颗粒间夹带的二 硫化碳气体和半焦颗粒微孔内吸附的二硫化碳气体置换出去， 避免含炭固体物 质夹带大量二硫化碳气体迸入加热炉燃烧，'产生大量 sox， 同时降低产品收率。 所述预提升器的作用是把热炭管线来的含炭固体物质提升上去，使之向上运动， 并形成理想的活塞流， 以提高喷嘴来的雾化液态硫磺与含炭固体物质的接触效 率。
料仓里的含炭固体物质经加料器输送至流化床加热炉内， 经空气流化燃烧 后烧掉一部分含炭固体物质， 放出热量加热其余含炭固体物质； 被加热的含炭 固体物质经热炭管线进入预提升器， 然后进入提升管并向上流动； 气态或液态 硫磺由喷嘴喷入提升管内， 与高温含炭固体物质接触并反应， 生成气态二硫化 碳； 设置在提升管末端的快分装置将生成的气态二硫化碳与未反应完的含炭固 体物质进行分离， 分离出的气态二硫化碳夹带部分含炭固体物质进入沉降器， 然后进入旋风分离器分离掉夹带的含炭固体物质， 由沉降器顶部排出， 进入后 续的分离系统； 被快分装置分离下来的未反应完的含炭固体物质落入沉降器下 方的汽提段,经惰性气体汽提掉夹带的二硫化碳气体后由冷炭管线进入流化床 加热炉内燃烧。 为了避免流化床加热炉内的含炭固体物质燃烧不充分而产生一 氧化碳， 随即直接排入空气而造成环境污染的问题， 人们可采用多种方法将产 生的高温烟气进行处理， 这些方法是本领域的普通技术人员所公知的。
本发明所述设备包含两种形式， 分别是并列式和同轴式， 其中并列式结构 如下： 流化床加热炉与沉降器并列布置， 其中预提升器、 提升管和沉降器为同 轴布置， 由下向上的顺序依次为： 预提升器、 提升管和沉降器； 提升管上端直 接插入沉降器下部， 热炭管线和冷炭管线分别为斜管， 若空间不够， 则将冷炭 管线和热'炭管线的进、 出口设置为斜管， 中间为直管。 而同轴式的具体结构如 下： 流化床加热炉与沉降器同轴布置， 其中预提升器与提升管同轴布置， 沉降 器位于流化床加热炉上方，提升管由竖管和横管构成，横管前端伸入沉降器内， 冷炭管线设置在流化床加热炉内， 其出口处设有防倒锥， 以防止流化床加热炉 内的气体窜入冷碳管线内， 为现有公知产品， 热炭管线由竖管和斜管构成。
对于并列式结构， 与汽提段连接处冷炭管线与汽提段轴线的角度控制在
20°〜60°之间， 与流化床加热炉连接处热炭管线与流化床加热炉轴线的角度控 制在 20。〜60。之间； 本发明所述流化床加热炉的结构有三种结构形式， 一是流 化床加热炉上部与下部同直径； 二是其上部直径小于下部直径， 以增加稀相速 度， 人为降低旋风分离器效率， 将燃烧后的飞灰排出； 三是下部直径小于上部 直径， 主要是为了减小稀相气体速度， 减小夹带的颗粒浓度， 提高旋风分离器 效率。
无论对于并列式结构或是同轴式结构， 提升管中部增设流化床层， 其目的 是为了延长反应时间， 流化床层的直径大于提升管直径， 流化床层的直径及其 大小由所需的反应时间确定； 为维持流化床层料位， 流化床层与沉降器下方的 汽提段之间通过圆管连通， 圆管上装有阀门。
为了便于调节含炭固体物质的流量， 冷炭管线和 /或热炭管线上分别装有控 制阀， 该控制阀可为滑阀或塞阀或其它控制高温颗粒流量的阀门； 当设备并列 式布置时， 冷炭管线和热炭管线上分别装有控制阀； 当设备同轴式布置时， 由 于冷炭管线位于硫化床加热炉内， 所以热炭管线上装有控制阀。
上述旋风分离器为外旋风分离器或内旋风分离器， 旋风分离器内部设置有 隔热、 耐磨衬里， 旋风分离器为一级旋风分离器， 或多级旋风分离器串联， 其 中每一级旋风分离器为一个或多个， 具体个数由沉降器内气体流量及沉降器尺 寸决定； 快分装置为旋风分离器或三叶形快分或旋流快分等气固分离设备。
与现有技术相比， 本发明具有以下优点：
1、采用预提升器及提升管使含碳固体物质与液态或气态硫磺在提升管内充 分接触并发生反应， 同时提升管中部的流化床层使得反应进行地更彻底， 大大 提高了反应物的接触效率， 增加了产品的收率；
2、相对于原有流化床工艺所要求的硫磺气化是必须步骤，本发明所述硫磺 可以为液态， 不仅所需温度较低， 能耗低， 而且所需设备简单， 占地较小， 减 少生产成本；
3、汽提段的设置使得未反应完全的含炭固体物质中夹带的二流化碳气体被 汽提掉， 有效避免大量二硫化碳气体进入加热炉燃烧， 产生大量 S0X， 从而减少 污染， 保护了环境， 同时提高了产品收率；
4、整个装置结构简单、 省材料、造价低、 易制作， 有利于实现连续化、 自 动化生产， 并有利于生产过程的环保处理。
总之， 采用本发明所述设备生产二硫化碳， 在技术上和经济上都是最佳的 选择， 真正实现了节能、 降耗、 清洁、 环保的目标。
附图说明 图 1为本发明所述的并列式结构示意图之一
图 2为本发明所述的并列式结构示意图之二
图 3为本发明所述的并列式结构示意图之三
图 4为本发明所述的并列式结构示意图之四
图 5为本发明所述的同轴式结构示意图之一
图 6为本发明所述的同轴式结构示意图之二
图中： 1-料仓， 2-加料器， 3-流化床加热炉， 4-热炭管线， 5-预提升器， 6- 提升管， 7-喷嘴， 8-沉降器， 9-快分装置， 10-旋风分离器， 11-汽提段， 12-冷炭 管线， 13-防倒锥， 14-流化床层， 15-圆管， 16-控制阀， 17-阀门。
具体实施方式
实施例 1: 如图 1所示， 为本发明所述的并列式结构
循环流化床制备二硫化碳的设备， 包括料仓 1、 加料器 2以及通过管线与 加料器 2连接的流化床加热炉 3， 流化床加热炉的下部直径小于上部直径； 流 化床加热炉 3下方设有热炭管线 4， 热炭會线 4另一端与预提升器 5连通， 预 提升器 5上方连有提升管 6，提升管 6上设有喷嘴 7，提升管 6上端伸入沉降器 8， 末端设置快分装置 9， 该快分装置为旋风分离器， 沉降器内顶部设有旋风分 离器 10， 内下方设有汽提段 11，汽提段 11下方设有与流化床加热炉 3连通的 冷炭管线 12，冷炭管线 12和 /或热炭管线 4上分别装有控制阀 16。如图 1所示， 并列式的结构体现在流化床加热炉 3与沉降器 8并列布置， 其中预提升器 5、 提升管 6和沉降器 8为同轴布置， 提升管 6上端直接插入沉降器下部， 热炭管 线 4和冷炭管线 12分别为斜管，与汽提段 11连接处冷炭管线 12与汽提段轴线 的角度控制在 20°〜60°之间， 与流化床加热炉 3连接处热炭管线 4与流化床加 热炉轴线的角度控制在 20°〜60°之间。
具体实施时， 料仓里的含炭固体物质经加料器输送至流化床加热炉内， 经 空气流化燃烧后烧掉一部分含炭固体物质， 放出热量加热其余含炭固体物质； 被加热的含炭固体物质经热炭管线进入预提升器，然后进入提升管并向上流动； 气态或液态硫磺由喷嘴喷入提升管内， 与高温含炭固体物质接触并反应， 生成 气态二硫化碳； 设置在提升管末端的快分装置将生成的气态二硫化碳与未反应 完的含炭固体物质进行分离， 分离出的气态二硫化碳夹带部分含炭固体物质进 入沉降器， 然后进入旋风分离器分离掉夹带的含炭固体物质， 由沉降器顶部排 出， 进入后续的分离系统； 被快分装置分离下来的未反应完的含炭固体物质落 入沉降器下方的汽提段， 经惰性气体汽提掉夹带的二硫化碳后由冷炭管线进入 流化床加热炉内燃烧。
实施例 2: 如图 2所示， 为本发明的并列式结构
与实施例 1的区别仅在于流化床加热炉的上部直径小于下部直径， 在实际 操作中以增加稀相速度， 人为降低旋风分离器效率， 将燃烧后的飞灰排出。
实施例 3: 如图 3所示， 为本发明的并列式结构
与实施例 1的区别在于提升管 6中部增设流化床层 14， 以延长反应时间， 流化床层的直径大于提升管直径， 流化床层的直径及其大小由所需的反应时间 确定； 为维持流化床层料位， 流化床层与沉降器下方的汽提段之间通过圆管连 通， 圆管上装有阀门， 可控制料体流量。
实施例 4: 如图 4所示， 为本发明的并列式结构
与实施例 3的区别仅在于流化床加热炉的上部直径小于下部直径。
实施例 5: 如图 5所示， 为本发明的同轴式结构
循环流化床制备二硫化碳的设备， 包括料仓 1、 加料器 2以及通过管线与 加料器 2连接的流化床加热炉 3，流化床加热炉 3下方设有热炭管线 4，热炭管 线 4另一端与预提升器 5连通， 预提升器 5上方连有提升管 6, 提升管 6上设 有喷嘴 7, 提升管 6上端伸入沉降器 8， 末端设置快分装置 9， 该快分装置为三 叶形快分，沉降器内顶部设有旋风分离器 10， 内下方设有汽提段 11，汽提段 11 下方设有与流化床加热炉 3连通的冷炭管线 12， 冷炭管线 12和热炭管线 4上 分别装有控制阀 16。 如图 5所示， 同轴式的结构体现在流化床加热炉 3与沉降 器 8同轴布置， 其中预提升器 5与提升管 6同轴布置， 沉降器 8位于流化床加 热炉 3上方， 提升管 6由竖管和横管构成， 横管前端伸入沉降器内， 冷炭管线 12设置在流化床加热炉 3内，其出口处设有防倒锥 13， 热炭管线 4由竖管和斜 管构成。
同轴式结构中， 含炭固体物质流动途径、硫磺进料方式、反应和燃烧方式， 即整个制备过程是和并列式一致的。
实施例 6: 如图 6所示， 为本发明的同轴式结构
与实施例 5的区别仅在于提升管 6的竖管中部增设流化床层 14， 以延长反 应时间， 流化床层的直径大于提升管直径， 流化床层的直径及其大小由所需的 反应时间确定； 为维持流化床层料位， 流化床层与沉降器下方的汽提段之间通 过圆管 15连通， 圆管上装有阀门 17。 '

Claims

权 利 要 求
1、一种循环流化床制备二硫化碳的设备， 其特征是包括料仓（1 )、 加料器 (2)以及通过管线与加料器（2)连接的流化床加热炉（3)， 流化床加热炉（3) 下方设有热炭管线 （4)， 热炭管线 （4) 另一端与预提升器 （5)连通， 预提升 器（5)上方连有提升管（6)， 提升管（6)上设有喷嘴（7), 提升管（6)上端 伸入沉降器 (8),末端设置快分装置（9)，沉降器内顶部设有旋风分离器（10)， 内下方设有汽提段 （11 ), 汽提段 （11 )下方设有与流化床加热炉 （3)连通的 冷炭管线 （12)。
2、根据权利要求 1所述的循环流化床制备二硫化碳的设备，其特征是流化 床加热炉（3 )与沉降器（8)并列布置， 其中预提升器（5)、 提升管（6)和沉 降器（8) 为同轴布置， 提升管（6)上端直接插入沉降器底部， 热炭管线（4) 和冷炭管线 （12)分别为斜管。
3、根据权利要求 1所述的循环流化床制备二硫化碳的设备，其特征是流化 床加热炉 （3)与沉降器（8) 同轴布置， 其中预提升器（5) 与提升管（6) 同 轴布置， 沉降器（8)位于流化床加热炉（3 )上方， 提升管（6) 由竖管和横管 构成， 横管前端伸入沉降器内， 冷炭管线 （12) 设置在流化床加热炉 （3) 内， 其出口处设有防倒锥（13)， 热炭管线（4) 由竖管和斜管构成。
4、根据权利要求 2所述的循环流化床制备二硫化碳的设备，其特征是与汽 提段（11 )连接处冷炭管线 （12)与汽提段轴线的角度控制在 20°〜60°之间， 与流化床加热炉 （3 )连接处热炭管线 （4) 与流化床加热炉轴线的角度控制在 20°〜60°之间。
5、根据权利要求 2所述的循环流化床制备二硫化碳的设备，其特征是流化 床加热炉（3 )上部与下部同直径或上部直径小于下部直径或下部直径小于上部 直径。
6、根据权利要求 1或 2或 3所述的循环流化床制备二硫化碳的设备，其特 征是提升管（6) 中部增设流化床层 （14)。
7、根据权利要求 6所述的循环流化床制备二硫化碳的设备，其特征是流化 床层（14)与沉降器（8)下方的汽提段之间通过圆管（15)连通， 圆管上装有 阀门 （17)。
8、根据权利要求 1或 2或 3所述的循环流化床制备二硫化碳的设备，其特 征是冷炭管线 （12) 和 /或热炭管线（4) 上分别装有控制阀 （16)。
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